Method for the adsorptive drying of purified biogas and for regenerating laden adsorbents

ABSTRACT

In a method for adsorptively drying purified biogas and regenerating laden absorbents, foreign matter is not allowed to enter the purified biogas, the content of methane in the gas remains virtually unchanged and the effort involved in regenerating the laden adsorbent is reduced. Drying and regeneration are effected in a closed biogas cycle, wherein separate layers based on silica gel and molecular sieves are used as the adsorbent. The biogas to be dried first flows through the silica gel layer. The adsorbent is regenerated with exclusively heated, dried biomethane having a temperature of up to 150° C. which, after contact with adsorbent, is recirculated to the outflow of purified biogas. After regeneration, the bed is cooled by biomethane, which is subsequently recirculated to the outflow of purified biogas. Methane-containing water accumulating during drying and regeneration is recirculated to the biogas generation and/or purification.

BACKGROUND OF THE INVENTION Field of the Invention

The invention relates to a process for adsorptive drying of purifiedbiogas (called biomethane) and regeneration of laden adsorbents, whereinthe dried biogas is sent to a further use, for example by feeding into aconventional natural gas grid.

Biogas can be purified by different processes, with the aim of obtaininga gas with a relatively high proportion of methane, in the range from 90to 99% by volume.

After the purification, biomethane may still comprise, as residualconstituents, carbon dioxide (0.1 to 4% by volume), hydrogen (0.01 to0.2% by volume), nitrogen and oxygen (0.2 to 4% by volume) and water (1to 3% by volume). Further components, for example H₂S, NH₃, may still bepresent in the range from 1 to 5 ppm. Depending on the fermentationprocess, the purified biogas (biomethane) may still contain proportionsof aromatic or other hydrocarbons, in amounts of up to 1000 ppm, withignition points well below that of methane.

For a further use of biomethane, for example for feeding into a naturalgas grid, it is necessary to remove water present in the gas down to alimit of below 40 mg/m³ (STP).

For drying or demoisturization of biogas, processes for cooling andcondensation and for adsorption and absorption are already known. Thecooling is usually effected within underground pipes provided with acondensate separator at the lowest point. If required, water coolers canadditionally be used. Adsorption processes are effected using specificadsorbents, such as activated carbon, molecular sieves or silica gel.After the loading, the adsorbents can be regenerated by heating.

Absorptive processes (EP 0 907 400 B1) work with a solvent such astriethylene glycol, and gas scrubbing results in dissolution of waterpresent in the gas triethylene glycol, which can subsequently beregenerated again at a temperature of 200° C.

This procedure is very energy-intensive since water bound in thetriethylene glycol has to be evaporated (distilled off). Since methaneis soluble in triethylene glycol (approx. 30 g/l at 1 bar and 25° C.),methane losses have to be expected.

DE 103 59 959 B4 proposes using undried, moist biogas for regenerationof the moist triethylene glycol desiccant.

DE 20 2008 012 371 U1 discloses an apparatus for adsorptive drying ofbiogas in a fixed bed (molecular sieves), using electrodes which areconnected to an HF generator for supply of HF voltage to heat the fixedbed. The additional heating of the solid bed by means of HF energy isassociated with a high level of complexity. Moreover, there is aconsiderable safety risk since particular substances with a tendency toself-ignite may be present in the biogas or natural gas.

BRIEF SUMMARY OF THE INVENTION

It is an object of the invention to provide a process for adsorptivedrying of purified biogas having a methane content of at least 90% byvolume and regeneration of laden adsorbents, in which no extraneoussubstances can get into the purified biogas, the proportion of methanepresent in the gas to be purified remains present virtually unchanged,and the complexity for regeneration of the laden adsorbent is reduced.

According to the invention, the object is achieved by the features asclaimed. Advantageous configurations and developments of the procedureare the subject to dependent claims.

For adsorptive drying of purified biogas (biomethane), the adsorbentsused are separate layers based on silica gel and molecular sieves, thebiogas to be dried flowing first through the silica gel layer. The layerof silica gel preferably consists of two layers, a lower macroporouslayer and an upper mesoporous layer. A ratio between the lower layer tothe upper layer lies between 1:1 and 1:4. The vol ime ratio of first“silica gel” layer to second “molecular sieves” layer is 20:1 to 3:1,preferably 12:1 to 8:1. This depends on the water content of the biogasto be dried (biomethane). The higher the water content in the biogas tobe dried, the greater the ratio thereof.

The layer of silica gel may also be formed from at least two layers ofdifferent silica gels, the space between these two layers being heatedby means of an external heat source. This can be accomplished by meansof an installed intermediate heater.

This measure can achieve water contents in the biogas of below 10 mg/m³(STP) and dew points of −60° C. to −80° C.

The biogas to be dried is preferably pumped through the adsorber atambient pressure. If required, a pressure of up to 1 bar can also beemployed. Prior to the drying of the purified biogas (biomethane), thewater content should already be reduced down to 5 g/m³ (STP). This canbe accomplished, for example, by cooling down to 10 to 30° C with cooledbiomethane. Without prior drying, correspondingly greater dimensions ofthe adsorbers are required. The adsorption time is 12 to 14 hours.Within this time, the water content in the dried biomethane can bereduced down to well below 20 mg/m³ (STP).

For subsequent regeneration of the adsorbent, exclusively heated driedbiomethane is used, and this is recycled back into the starting streamof purified biogas after the contact with adsorbent. The heating ispreferably effected to a temperature of approx. 110 to 150° C. in aseparate heat exchanger by means of a heat carrier, such as thermal oilor hot water or steam. For this purpose, exact temperature control isrequired in order to avoid self-ignition of hydrocarbons present in thebiomethane. The temperature of the heat carrier should not exceed 200°C. During the regeneration of the bed, the temperature of the exitingbiomethane is measured continuously. During the regeneration, this iswithin a range from 20 to 30° C. If the exit temperature rises to 40 to50° C., the supply of biomethane is shut down and the regenerationprocess is ended.

It is advantageous when the adsorber is heated at least in the lowerregion on commencement of the regeneration. This can be accomplished bymeans of a jacket or a heating coil through which a heat carrier mediumflows. Additional heating of the adsorber during the first hour ofregeneration is already sufficient.

The duration of indirect heating of the adsorber should be at least 30minutes. The heat carrier medium should have an of temperature 70 to180° C.

The areas to be heated should be at least 10% of the adsorber height.

Under these conditions, it was found that, for a given heat input, thedrying time for the laden bed can be reduced by up to 50%. This isachieved, more particularly, by faster introduction of the heat requiredto heat the adsorbers than customary to date via the drying gas stream.Thus, the drying process proceeds much more effectively in the region ofthe macroporous silica gels, i.e. where the greatest amount of water isbound. The indirect heating of the adsorber during the drying step isrequired only over a period of up to 1 hour. Thereafter, the heating canbe switched off.

For direct reuse of the adsorber for drying purified biogas(biomethane), cooling of the bed to standard temperature is required.For this purpose, purified biogas (biomethane) is used, which is cooleddown to 5 to 15° C. in a separate heat exchanger and passed through thebed. After about two hours, the temperature of the bed is again withinthe desired range. The biomethane used for regeneration and cooling issent back to the starting stream of purified biogas. In the individualprocess stages, predrying and regeneration, water obtained is collectedand recycled back into the circuit for production and/or purification ofbiogas.

The advantage of the process proposed is that of a closed biogascircuit. Since the adsorbent is regenerated exclusively with purifiedbiogas, absolutely no extraneous substances can get into the biomethaneduring the drying. The dried biomethane can thus be fed without anyproblem, if appropriate after a pressure increase, into a natural gasgrid, or can be sent to another use. In the case of recycling of thecondensate obtained during the drying into a preliminary stage forbiogas production, there are no methane losses. This procedure is thusvery economically viable. The selected combination of the composition ofthe adsorber bed, in terms of activity, is matched to the amount ofwater to be removed and the regeneration conditions. The water contentin the purified biogas (biomethane) can thus be reduced from approx. 5g/m³ (STP) down to at least 10 mg/m³ (STP) or even lower, and theduration up to maximum loading and the duration for a thermally gentleregeneration (temperature max. up to 150° C.) and cooling of the ladenbed can be kept about the same. Under thermally more favorableconditions, indirect heating of the adsorber, the regeneration time forthe laden adsorber column can be reduced even further.

The mass transfer which takes place during the loading, the transfer ofthe water from the biogas to the adsorbents, shifts until the end of theadsorber column is reached and there is breakthrough of the moistbiogas, but this is ruled out in practice by an early termination. Thebed of molecular sieves disposed at the end extends the active masstransfer zone. The water absorption proceeds at first through the silicagel up to equilibrium. The next layer of molecular sieves absorbs watermore slowly, but the loading capacity increases overall and enables theattainment of the low residual water contents of approx. 10 mg/m³ (STP).On attainment of this value, the drying is ended without reaching theupper limit in the absorption capacity. Only thus is sufficientregeneration of the molecular sieves enabled at comparatively lowtemperatures (max. up to 150° C.). Higher regeneration temperatureswould be prevented by the use of biomethane due to the self-ignitionrisk.

Application of a reduced pressure during the regeneration allows theremoval of water to be improved, and may make it possible to work atlower regeneration temperatures.

The invention is illustrated hereinafter by two examples. Theaccompanying drawing shows the function circuit diagram of a plant forperformance of the process.

BRIEF DESCRIPTION OF THE EXAMPLES Example 1

A: Drying

Biogas produced from biological waste material in a fermenter ispurified to free it of unwanted secondary constituents, with removal ofcarbon dioxide present by means of an ambient pressure amine scrubbing.From the scrubbing column, 30 m³ (STP)/h of purified biogas, calledbiomethane, are drawn off at a temperature of 38° C. The biomethane hasthe following composition:

CH₄ 95.2% by vol. CO₂ 0.5% by vol. H₂O 4.0% by vol. O₂ 0.1% by vol. N₂0.2% by vol. H₂S 2 ppm NH₃ 1 ppm

The biomethane drawn off via line 1 is cooled in a first heat exchangerW1 to approx. 22° C. and then passed via line 2 to the downstream,second heat exchanger W2 and cooled therein down to 5° C. This reducesthe water content in the biomethane from originally 19 500 mg/m³ (STP)down to 5035 mg/m³ (STP). Via lines 9 and 10, separated water is removedto a non-illustrated vessel, optionally stored intermediately, and sentback to the biogas production or purification.

The amount of biomethane is reduced to 28.99 m³ (STP)/h. The compositionof the biomethane removed via line 3 has changed as follows:

CH₄ 98.52% by vol.  CO₂ 0.52% by vol. H₂O 0.66% by vol.

To dry the biomethane, two identical adsorbers A1 and A2 with a bedheight of 700 mm and a diameter of 300 mm, arranged downstream, are usedalternately for drying of the biomethane and, after loading, subjectedto a regeneration. While one adsorber is in drying operation, the otheradsorber is being regenerated.

Both adsorbers A1 and A2 contain a loose bed consisting of two differentadsorbents S1 and S2. The lower bed S1 consists of 20 l of silica gelwith a mean pore diameter of >50 to 100 nm (macropores) and 30 l ofsilica gel with a mean pore diameter of 25 nm (mesopores), which areseparated by a gas-permeable plate. The orifices in the plate are sosmall that mixing of different silica gel particles is impossible.

Above the mesoporous silica gel bed is disposed a bed S2 of molecularsieves (zeolites) with a pore diameter of 0.4 nm, in an amount of 5 l.The silica gel bed and the molecular sieves are separated by agas-permeable plate, such that the particles cannot mix. The ratio ofbed S1:bed S2 is 50:5=10.

In continuous operation, the biomethane is supplied via line 3 to one ofthe two adsorbers A1 or A2, for example to adsorber A1, and is driedduring contact with the adsorbents. At the same time, i.e. in parallel,the other adsorber A2, which has been laden in the meantime, isregenerated.

After leaving the second heat exchanger W2 at a temperature of 5° C.,the biomethane to be dried flows from the bottom through the bed in theadsorber column A1 and is drawn off at the top of the adsorber A1 vialine 4. The drying is in principle effected at ambient pressure; onlythe suction pressure for conveying the gas stream is applied, and thisis approx. 10 mbar.

According to the specific application, the dimensions of the adsorbercolumn and the flow rate are determined experimentally, withconsideration of maximum effectiveness of the mass transfer zone.

The specific selection and composition of the adsorbents enables arelatively long utilization time. Only after an adsorption time of 14hours is there breakthrough of the moist gas with the consequence ofdiversion of the gas stream to the other adsorber column 2 which hasbeen regenerated in the meantime. During the first 14 hours of theadsorption, the water content in the dried biomethane is only 10 mg/m³(STP) (dew point −63° C.). The dried biomethane drawn off aftercompression via line 5 (temperature approx. 25° C.) can be fed directlyinto a natural gas grid.

If the adsorption time were to be prolonged by approx. 1 hour to 15hours, the water content in the dried biomethane increases up to 153mg/m³ (STP) (dew point −40° C.).

B: Regeneration

During the drying of the biomethane which takes place in one adsorbercolumn A1, the laden adsorber column A2 is regenerated as follows:

Downstream of the compressor V1, a closable branch line 6 isincorporated into the line 4 for removal of the dried biomethane, andthis can be used to separate out 5 m³/h of dried biomethane. Thissubstream is passed through a third heat exchanger W3 and heated up to atemperature of approx. 120° C. and passed through line 7 to the adsorberto be regenerated. The hot substream of dried biomethane, forregeneration of the adsorber particles, is passed from the top throughthe laden adsorber column A2 and absorbs the moisture present in theseparticles while being cooled. The substream determined for theregeneration is pumped through the adsorber column at a pressure of 40mbar.

After a regeneration time of approx. 12 hours, the adsorber bed againhas sufficient loading capacity. The moisture-laden biomethane is sentback to the biomethane gas stream to be dried in the circuit.

For direct reuse of the adsorber bed for drying, however, cooling of theadsorbents is still required. For this purpose, the dried biomethaneseparated out via line 6 is not heated but passed directly through afourth heat exchanger W4 and cooled therein to approx. 10° C., andpassed through the bed in the adsorber A2. The cooled biomethane istransported via line 7. The biomethane used for cooling is recycled vialine 11 back into the biomethane circuit. A cooling time of 2 hours isfollowed by switching from adsorber A1 to adsorber A2. The ladenadsorber A1 is now regenerated and the adsorber A2 is used for drying.

Based on the starting amount of biomethane to be dried (approx. 30 m³(STP)/h), 1.2 l/h of water with a methane content of 28 g/l aredischarged via lines 9 and 10. The water can be collected and then sentdirectly back to the biogas purification as scrubbing water. The amountof methane present in the condensate is 0.034 kg/h or 0.024 m³ (STP)/h.This corresponds to a proportion of 0.084% of the amount of methane tobe dried. The advantage of this procedure is that no methane lossesoccur.

In the case of plants with drying of approx.

5000 m³ (STP)/h of methane, there would otherwise be methane lossesamounting to 4 m³ (STP)/h.

Example 2

The regeneration of the laden adsorber column is conducted under thesame conditions as in example 1, with additional heating, during thefirst hour, of the lower section (up to a height of approx. 300 mm) ofthe adsorber column with a liquid heat carrier having a temperature of150° C. At the same time, as in example 1, 5 m³/h of dried biomethane ata temperature of approx. 120° C. and a pressure of 40 mbar are passedthrough the bed of the adsorber column.

The indirect additional heating accelerates the drying process for thesilica gel bed which comprises the greater proportion of water ormoisture.

Since the heating of the adsorber column already drives out a portion ofthe moisture present in the silica gel, the heat present in the dryinggas (biomethane) can thus be utilized more effectively for the furtherdrying of the bed, since the adsorber is already heated by the indirectheating in the region where the greatest proportion of moisture ispresent.

After a drying time of approx. 8 hours, the adsorber bed has againattained adequate loading capacity and is cooled for another two hoursin an analogous manner to that in the example. After 10 hours ofregeneration, the adsorber bed is again fully usable. In the case ofsubsequent use of the adsorber column, it was found that the bed has amuch higher loading capacity compared to example 1.

During the first 14 hours of the adsorption of the biogas to be dried,the water content in the dried biomethane is only 4 mg/m³ (STP) (dewpoint −70° C.). In the case of extension of the adsorption time byapprox. 1 hour to 15 hours, the water content in the dried biomethaneincreases up to 10 mg/m³ (STP) (dew point −63° C.).

This example shows that, in the case of use of indirect adsorberheating, much better drying can be achieved with lower water contentsand a shorter drying time.

Example 3

Under the same conditions as in example 2, the regeneration temperatureis now increased from 120 to 140° C.

Under these conditions, the water content in the dried biomethane up to10 hours is 50 to 80 mg/m³ (STP), then it rises to 160 mg/m³ (STP)within 1 hour.

This shows that, in spite of higher energy expenditure of example 2,only a small improvement in the drying can be achieved. In the case ofuse of higher regeneration temperatures, the adsorber bed is damaged. Anincrease in the drying gas rate via line 4 from 5 to 10 m³ (STP)/hreduces the water content in the dried biomethane to 40 to 70 mg/m³(STP) over the first 10 hours, but requires twice the regenerationpower.

DESCRIPTION OF THE INVENTION Comparative Example 1

In contrast to example 1, the moist biomethane is dried using only onebed consisting of 55 l of silica gel with a pore diameter of 25 nm.

Under the same conditions as in example 1, breakthrough of the moist gasoccurs after an adsorption time of only 10 hours.

In the dried biomethane, a residual water content of 100 to 120 mg/m³(STP) is found over the adsorption time.

Comparative Example 2

Under the same conditions as in example 2, the desiccant used is now 20l of silica gel with a pore diameter of 50-100 nm followed above by only35 l of silica gel with a pore diameter of 25 nm.

Under these conditions, the water content in the dried biomethane is 40to 50 mg/m³ (STP) up to 12 hours, then it rises to 145 mg/m³ (STP)within 1 hour.

The invention claimed is:
 1. A gas drying process, comprising: providinga purified biogas having a methane content of at least 90% by volume;providing an adsorber with adsorbents in the form of separate layersbased on silica gel and molecular sieves; adsorptively drying thepurified biogas with the adsorbents and regenerating laden adsorbents ina closed biogas circuit; and conducting the biogas to be dried firstthrough a layer of silica gel, and wherein regenerating furthercomprises regenerating the adsorbent using exclusively heated driedbiomethane having a temperature of up to 150° C. and, after contact withthe adsorbent, recycling the biomethane back into a starting stream ofthe purified biogas; and on completion of regeneration, contactingcooled dried biomethane with the adsorbent and recycling back into thestarting stream of the purified biogas, and conductingmethane-containing water obtained during the drying and regenerationback to a biogas production and/or purification.
 2. The processaccording to claim 1, which comprises removing a portion of water bycooling the purified biogas prior to supplying the purified biogas tothe adsorber.
 3. The process according to claim 1, wherein the layer ofsilica gel is formed from at least two layers including a lowermacroporous layer and an upper mesoporous layer, with a volume ratiobetween the lower layer to the upper layer lying between 1:1 and 1:4. 4.The process according to claim 1, which comprises passing the biomethanefor the regeneration through a bed of the adsorbent at a temperature of110 to 150° C., with a continuous measurement of the temperature of theexiting biomethane, and a shutdown of a supply of biomethane after arise in the exit temperature to 40 to 50° C.
 5. The process according toclaim 1, which comprises pumping the biogas to be dried through theadsorber at ambient pressure or with a slightly elevated pressure of upto 1 bar.
 6. The process according to claim 1, wherein a volume ratio ofa first layer being the silica gel layer to a second layer being themolecular sieves is 20:1 to 3:1.
 7. The process according to claim 1,which comprises carrying out the adsorption during an adsorption timebetween 12 and 14 hours and thereby reducing a water content in thedried biomethane to below 20 mg/m³ (STP).
 8. The process according toclaim 1, which comprises cooling the regenerated adsorbents, prior toreuse, down to 10 to 30° C. with cooled biomethane.
 9. The processaccording to claim 8, which comprises cooling the regenerated adsorbentswith cooled biomethane having a temperature of between 5 and 15° C. 10.The process according to claim 1, which comprises indirectly heating atleast a lower region of the adsorber during the regeneration.
 11. Theprocess according to claim 1, which comprises regenerating the ladenadsorber under reduced pressure.